CN101605589B - Method and device for purifying the flue gases of a sintering process of ores and/or other metal-containing materials in metal production - Google Patents

Method and device for purifying the flue gases of a sintering process of ores and/or other metal-containing materials in metal production Download PDF

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CN101605589B
CN101605589B CN2007800513602A CN200780051360A CN101605589B CN 101605589 B CN101605589 B CN 101605589B CN 2007800513602 A CN2007800513602 A CN 2007800513602A CN 200780051360 A CN200780051360 A CN 200780051360A CN 101605589 B CN101605589 B CN 101605589B
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CN101605589A (en
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霍斯特·格罗霍夫斯基
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/08—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
    • B01D53/12—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents according to the "fluidised technique"
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B01D53/685—Halogens or halogen compounds by treating the gases with solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/81—Solid phase processes
    • B01D53/83—Solid phase processes with moving reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/025—Other waste gases from metallurgy plants
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

The invention relates to a method for scrubbing effluent gases from a sintering process for ores in metal production, in which ore material is sintered with a solid fuel by combustion of the solid and passing through a carbonisation process, wherein at least the pollutants SOx and/or HCl and NOx are reduced or essentially removed. The sinter effluent gas is introduced into a moving bed reactor (50) from below through a lower and an upper layer (54B; 54A) of adsorption and/or absorption agent which is already charged with NOx and SOx and/or HCl, wherein at least the majority of the SOx and/or HCI components from the sinter effluent gas are absorbed in the pore system of the adsorption and/or absorption agent charged with NOx. The sinter effluent gas purified of the majority of the SOx and/or HCI components is homogeneously mixed with an ammoniacal compound such as ammonia or urea and admitted from below into the upper layer of adsorption and/or absorption agent already charged with NOx and small amounts of SOx and/or HCl from below through an upper horizontal gas influx and bulk material outlet floor (52A) of the moving bed reactor. On flowing through the upper layer (54A) at least the majority of NOx components from the sinter effluent gas is absorbed on the surface of the absorption/adsorption agent charged with NOx or N2 and small amounts of SOx and/or HCl. Fresh and/or regenerated adsorption/absorption agent is introduced via a bulk material distribution floor (50C) at the upper end of the moving bed reactor and continuously moves through the upper and lower layer of the whole moving bed reactor wherein firstly Nox and N2 and steam are absorbed on the surface thereof and then SOx and/or HCl are absorbed in the pore system thereof.

Description

Be used for purifying the method and apparatus of metal preparation by the waste gas that sintering process produced of ore and/or other metal-containing material
Technical field
The present invention relates to being used for purifying and preparing the method for the waste gas that process produced by ore sintering technology and according to claim 1 preamble according to the device of this method of enforcement of claim 11 preamble at metal.
Background technology
In the ore materials sintering, this material to be mixed with the solid that contains granule carbon and places on the sintering belt, under the partially combusted at least situation of this solid, this material is transported to discharge end in the process that on this sintering belt, is fed forward.Perhaps, raw material is granulated or briquetting, sintering then.Supply with combustion air.In sintering process, charging makes the raw material coalescence thus through glowing and partial combustion process at least, promptly sinters bigger piece into.Because the combustion air of supplying with increases the burning and the technology of glowing, so charging discharges a large amount of gases, and this gas removes component CO 2And possible CO, O 2, H 2O and/or N 2Also contain a series of pollutants outward.Especially, said pollutant is nitrogen oxide (NO x), SO 2, HCl 、 bioxin, furans, dust and the sublimable or coagulable residue, heavy hydrocarbon and/or the heavy metal that produce by the technology of glowing.
The research that air is kept shows, for example comprises substantially a big chunk of all dirt for preparing in the process to be produced at metal from the waste gas of sintering belt.Therefore, the pollutant more than 90% of corresponding emission is bioxin and furans in the production of iron and steel.Because the especially big exhausted air quantity of sintering belt device only just possibly carry out gratifying gas purification up to now under very large cost, this cost obviously increases the totle drilling cost that steel is produced.Especially and since in the sintering belt waste gas level of pollutant divide different with and form and very great fluctuation process arranged with charging, and because therefore very different reaction and the available purification methods of pollutant must implement a plurality of purifying step in succession.
Therefore, for example proposed so-called gas carrier method, leached gas current-carrying particle in downstream, and catalytic oxidation is carried out for reducing bioxin in downstream again.Adopt these methods the catalyst damage of certain degree can occur; This special realization is the surface coverage (Abschlussbericht50441-5/217 " Verringerung von Dioxinemissionen aus Sinteranlagen " im Auftrag des deutschen Bundesumweltamtes, Dezember 2002) of organic hydrocarbon to catalyst.
The another kind of exhaust gas purifying method that is used for the sintering belt device has been proposed among the WO 01/17663; This method is in gas current-carrying-purifying step, to purify sintering belt waste gas; Carry out the adsorption cleaning step subsequently; Wherein in gas current-carrying-purifying step, in waste gas, add (promptly than small grain size) the high value activated charcoal that grinds, to form gas current-carrying nebulous cloud thing.This adsorbent in small, broken bits the gas current-carrying mutually in react from the part of sintering belt waste gas pollutant to be removed.But subsequent reactions step as this gas current-carrying process; The dust that flies upward is not deposited on the cloth filter or on the electrofilter; But be deposited on the feed side of counter-flow moving bed reactor; The dust settling that flies upward this this is on the particle of moving bed bulk material, promptly in its surface or in intergranular space.Then, this sintering belt waste gas flows through the stratum granulosum as being made up of activated charcoal of counter-flow moving bed reactor so that this gas current-carrying in mutually before sintering belt waste gas experience adsorption cleaning through purifying.Gas current-carrying purification process in the moving-burden bed reactor downstream need use the second graininess cleanser, can not eliminate disadvantageous catalyst damage in the moving bed like this.
Particularly when from sintered discharge gas, removing NO xWhen very important, confirmed if from waste gas, remove NO by catalyst x, other pollutants such as SO 2With HCl interference is arranged especially, then in the sintered discharge gas contained these and other pollutant to removing NO xIt is so-called catalyst toxin.
Therefore, in WO 2006/084671 A1, adopt the preliminary clearning step with maximum remove particularly SO xAnd HCl, and adopt the after-purification step, wherein with being suitable for depositing NO xCatalyst such as carbon-bearing adsorbent flow through counter-current reactor from the top down.At this moment in single sorbing material layer, implement two step waste gas purification processes, wherein the first step is carried out in the inlet region, and second purifying step is carried out in the subsequent zone of this sorbing material layer.Show, wherein for example precipitate SO with calcium hydroxide 2The preliminary clearning step also be not enough because remain in the SO in the waste gas 2And/or the residual volume of HCl, if its be used to transform NO xRequired ammoniacal liquor contact then can cause at this NO xCatalyst is that this catalyst granules expands when containing absorbent carbon and/or adsorbent such as activated charcoal, and (the explosion particle forms, Popkornbildung).If in porous catalyst, form ammonia sulfate crystal or ammonia chloride crystal, also this effect can occur.The expansion that in pore system, forms crystal can make catalyst structure break.Therefore, this catalyst not only has been consumed, but also disintegration.And the granularity in the catalyst bed diminishes and can cause the pressure loss to increase, and causes the purification process cost to increase thus.According to WO2006/084671 A1,,, sintering belt waste gas purifies so reaching enough integral body because the impaired thus catalyst of the clean-up stage of single reactor beds bottom is discharged from the lower panel of this single reactor beds repeatedly.For the preliminary clearning of sintered discharge gas before getting into moving bed reactor device, preferably use bag hose or electrofilter and/or exhaust scrubber.As replacement scheme or as replenishing, can in the sintered discharge gas of gas current-carrying, add the reactant and/or absorbent such as pulverized limestone and/or the activated coke powdered carbon that segment cloth, before getting into moving bed reactor device, therefrom remove part pollutant SO at least at sintered discharge gas 2And HCl.Preferably, the previous SO of sintered discharge gas when getting into moving bed reactor device through purifying 2Content preferably is not more than the 5mg/ standard cubic meter less than the 100mg/ standard cubic meter.
The something in common of these known preliminary clearning steps is to carry out very big equipment cost for this reason, and must use other consumable material such as lime and disposal subsequently or further handle them.In addition, under the situation of wet washing, must overcome etching problem, heating problems and/or water treatment problems again.
Summary of the invention
Thus, the objective of the invention is purifying sintered discharge gas, particularly SO xAnd/or HCl and NO xProcess in avoid adopting the preliminary clearning step of using consumable material.For realizing this purpose, a kind of device that has the method for claim 1 characteristic and have claim 11 characteristic has been proposed.
Therefore, the present invention at first makes sintered discharge gas (maybe in advance dust removal step after) from following inflow moving-burden bed reactor, and the lower horizontal gas through this moving-burden bed reactor flows into bulk material discharges plate, and entering is by NO xOr N 2With possible steam and SO xAnd/or the absorption and/or the absorbent lower floor of HCl and possible other contaminants; In the process that flows through this absorption and/or absorbent lower floor, allow at least mainly to measure SO in the sintered discharge gas xAnd/or HCl composition and other possible pollutant are had NO by load xOr N 2Absorption and/or the pore system of absorbent absorb.Main amount SO xThe sintered discharge gas Free Surface in this absorption and/or absorbent lower floor that is cleaned with other possible pollutant leaves this layer, then fully to mix with ammonium-containing compound such as ammoniacal liquor or urea, with NO xChange into for example N 2And steam.That mix with ammonium-containing compound and mainly measure SO xAnd/or the sintered discharge gas that is cleaned of the HCl composition upper level gas that flows through same moving-burden bed reactor from below flows into bulk material and discharges plate, and entering is by NO xOr N 2With a small amount of SO xAnd the absorption of other possible contaminants and/or absorbent upper strata.In the process that flows through absorption and/or absorbent upper strata, the NO of main at least amount in the sintered discharge gas xComposition and at least a ammonium-containing compound are adsorbed on load has NO xOr N 2With a small amount of SO xAnd on the surface on the absorption of other possible pollutant and/or absorbent upper strata.Main amount SO xWith possible other pollutant and NO xThe sintered discharge gas that composition is cleaned Free Surface on absorption and/or absorbent upper strata leaves this layer, to leave this process subsequently.Absorption and/or the absorbent of fresh and/or regeneration be from top supply, and be evenly distributed on the last Free Surface on absorption and/or absorbent upper strata through the bulk material distribution grid of moving-burden bed reactor upper end.Absorption and/or absorbent are flowed into the closing device of discharging the plate district with bulk material by upper gas and interrupt, and little by little and fully pass through the upper and lower of whole moving-burden bed reactor from the top down, thus load NO at first in its surface xOr N 2And steam, then load SO in its pore system xWith other possible pollutant.Then, its lower gas through moving-burden bed reactor flows into and bulk material discharge plate.The replenishing of absorption and/or absorbent, discharge and translational speed preferably off and on (or continuously) through lower gas flow into bulk material discharge the plate below or lower gas flow into bulk material discharge plate on the realization of bulk material deliverying unit.Absorption and/or absorbent load SO in the upper strata of moving-burden bed reactor xWith the amount of possible other pollutant through corresponding be controlled at lower gas flow into bulk material discharge the plate below or lower gas flow into and bulk material discharge plate on the bulk material deliverying unit be adjusted to the amount that can be scheduled to respect to the absorption and/or the absorbent of load.
Simplified method greatly through the present invention, in single counter-flow moving bed reactor of two steps, made NO simultaneously xAnd SO xAnd/or HCl and other possible pollutant deposit cmpletely, and the adsorption/absorption capacity utilization rate of used absorption and/or absorbent is up to 100%.And the Dust Capacity that flows to moving-burden bed reactor that after preliminary clearning, still exists in the sintered discharge gas also is able to abundant removal.This effect is unexpected, though because in power plant's waste gas because the height of used carbon burning and than containing the obviously low pollutant of following in the sintering belt waste gas is removed SO simultaneously from fire coal-power plant's waste gas xAnd NO xOld adsorption method but need the high sorbent circulation amount of about twice.Same beat all be that the inventive method is compared and in the preliminary clearning step, removed SO described in WO 2006/084671 A1 xThe above-mentioned efficient of technology.Adopt this known method, in the preliminary clearning step every day the some tons of lime that must circulate.Comparatively speaking, though the present invention has NO at preload in the presence of ammonium-containing compound xWith deposit SO on the absorption of other pollutant and/or the absorbent x, but SO in the waste gas xRemoval reach comparable high level.Comparatively speaking, method is implemented simple, and has avoided absorption and/or the interference of absorbent in passing through two moved further bed bioreactor moving process.Replenishing of the absorption of using and/or the discharge of absorbent and fresh absorption and/or absorbent only controlled through the bulk material deliverying unit that below moving-burden bed reactor, exists, and will adsorb and/or the absorbent upper strata in load limitations arrive specific SO xAnd/or the degree of HCl amount.
If with the absorption of moving-burden bed reactor and/or the absorption in the absorbent upper strata and/or absorbent to SO xAnd/or the load value of HCl is limited in by the absorption of discharging from the bulk material deliverying unit and/or the weight maximum of absorbent to be 10 weight %, preferably to be 6 weight % to the maximum, then the NO in the sintered discharge gas xThe deposition degree is high especially, and can not damage the absorption of obstruction moving-burden bed reactor and/or the SO in the absorbent lower floor xAnd/or the absorption and/or the absorbent of HCl removal.This restricted passage bulk material deliverying unit control flows into through gas from the moving-burden bed reactor lower end and moving of plate of bulk material discharge realized.
If use carbon containing absorption and/or absorbent, then pollutant to be removed reaches extra high deposition degree in the sintered discharge gas.When absorption and/or absorbent when being activated charcoal, thus this absorption and/or absorbent through have two flow into and the approach of two moved further bed bioreactors of discharge plate and device for transferring in the favourable wearability of acquisition.If use the activated charcoal of moulding, then in two absorption and/or absorber layer, reach the suitable flow-rate ratio and the less pressure loss thus.But the granularity of carbon containing absorption and/or absorbent is wide variety basically.But preferably avoid the material of the so-called undersize of excessive particle and dust and form of chips as far as possible.Granularity is particularly advantageous between 1-10mm.But preferred close limit between 3-8mm also is preferred.For on identical absorption and/or absorbent, removing NO xAnd removal SO xAnd/or HCl, proved that granularity is 4-6mm, it is effective especially being preferably the 5mm order of magnitude.
Though absorption and/or absorbent can all be discarded after through moving-burden bed reactor; Particularly on sintering belt, burn; But the carbon containing absorption and/or the absorbent that confirm high value are particularly advantageous; Although because load in the present invention has extra high pollutant, it still can be reused after regeneration step.If use from top adding and with moving-burden bed reactor the so-called preactivated absorption that mixes mutually of the activated charcoal of having regenerated and/or absorbent as fresh absorption and/or absorbent; Then can be lower to the requirement of the activity of the absorption of fresh state and/or absorbent because activated charcoal after cycling through moving-burden bed reactor at every turn repeatedly the circulation of desorb and regeneration obtain sufficiently high activity.
Regeneration is preferably carried out through the regeneration step of 3 step process; The activated charcoal that wherein pollutant will be arranged from the load of moving-burden bed reactor is from the vertically extending regeneration unit of last introducing; At first pass through the desorption device such as the tubular type desorption device of indirect; Then from passing through the dusty gas of back degas zone, at last from cooler through indirect cooling with the sucking-off desorb.In this way, regeneration has the original creation meaning, and can be as construct in more detail by each measure described in the embodiment of Figure 1A desiredly.
Method of the present invention can be used as the gas treating process of bone dry, makes to have eliminated problem and the heating problems of using generations such as wet washing device.Preferably in moving-burden bed reactor more than 80 ℃ make method implement that very big flexibility is arranged with the gas temperature that is suitably 80-180 ℃, wherein 50-150 ℃, preferred 130-150 ℃ gas temperature produces particularly advantageous gas purification result.
If use according to the gas inflow/bulk material of WO 88/08746 A1 and discharge plate, then the adsorbent the upper and lower height in the moving-burden bed reactor is extremely uniform on reactor cross-section.Basically, the floor height in the moving-burden bed reactor also can change, and helps wherein or be unfavorable for that gas is discharged under the situation of size in space can extend or shorten the bulk material distributing pipe on each layer.But select fixing floor height usually.The present invention's floor height at the middle and upper levels is 1.5-4.5m, preferred 2.5-3.5m, especially preferably about 3m.Following layer height is preferably slightly smaller, is 0.5-3m, preferred 1.5-2m, especially preferably about 1.75m.These floor heights and floor height poor (between the upper and lower) make even implementation method simply still when the gas composition of sintered discharge gas changes.
Be used for NO xThe ammonium-containing compound that transforms and be adsorbed onto on the bulk material preferably is prepared as follows: in evaporimeter, will spray into solution such as the NH that contains ammonium through the other mixture that contains ammonium salt solution and air of heating 4In OH-solution and the compressed-air actuated mixture, form air/H 2O-steam/NH 3Gas mixture.Air/the H of this form 2O-steam/NH 3Gas mixture has original creation meaning of the present invention, and can such as hope ground implement in more detail by each measure described in the embodiment of Figure 1A.
" absorption " among the present invention is interpreted as the technology that one or more compositions quilts in the waste gas directly adsorb." absorption " among the present invention is interpreted as the at first after chemical reaction of material in the waste gas to be clean, only is adsorbed subsequently.According to the composition of sintered discharge gas, the doping of preference such as activated charcoal (mix or unadulterated) or carbon containing or unadulterated absorption and/or absorbent particularly the mixture of activated charcoal and reactant that is used for acid contaminant such as lime as absorption and/or absorbent.
This method can be implemented with the different operation mode, and irrelevant with used absorption and/or absorbent.
On the one hand, single pass refers to adsorb and/or the absorbent warp progressively shifts out the moving-burden bed reactor lower end and single passes through moving-burden bed reactor in that the upper end of bulk material layer is progressively additional, is not used further in this process afterwards.To having the situation that is the small amount of solid carrying capacity in very little stoichiometric factor and/or the fluid to be clean, particularly the situation of low amounts of dust carrying capacity is recommended to adopt such method of operation.
If the solid loadings of fluid, particularly dust carrying capacity are higher and/or if stoichiometric factor is not too favourable, can make absorption and/or absorbent several times cycle through moving-burden bed reactor so.After each circulation, absorption and/or absorbent can be then through handling to reuse.This processing for example can be: screening as use vibratory sieve, then or carry out dry elutriation simultaneously and stick to dust or the regeneration on absorption and/or the absorbing particles with the material of the undersize of deposition abrasion and/or deposition or mix to recover or to improve catalysis characteristics.Under these two kinds of operating positions (single or multiple use); Can make absorption and/or absorbent that long total residence time is arranged in reactor; Under the single pass situation, the time of staying in the course of reaction is long especially, i.e. absorption and/or the translational speed that exports from entering the mouth to of absorbent are less.Absorption and/or absorbent for example normally need under the high solids content of this fluid to be clean through reactor with higher translational speed.
By means of the present invention, can also be utilized in the relatively little advantage of stoichiometric factor of adsorbent in the preliminary clearning step (promptly more favourable economically) now, and needn't high flow rate absorption and/or next " exchanging for " this advantage of absorbed dose of radiation.Be implemented in the preliminary clearning step thus, particularly add in the sintered discharge gas before bag hose be selected from calcium oxide, calcium hydroxide, sodium acid carbonate and/or similarly alkali metal compound or alkaline earth metal compound material with sintered discharge gas in contained part SO x, HS and/or HCl combine.Preferred addition is corresponding to being preferably 1.0-2.5, the stoichiometric factor of preferred 1.5-2.0.The SO that preferably part is removed in the preliminary clearning step x, HS and/or HCl amount be contained SO in the sintered discharge gas x, HS and/or HCl 10-90%, preferred 50-80%, preferred especially 65-75%.Lower to the consumption maintenance of this material in the preliminary clearning step of the filtering material of other pollutant in dust load and the sintered discharge gas also like this with work, and obviously reduced the expensive absorption and/or the consumption of absorbent.
As it is said to implement scheme, and the parts for use that the used above-mentioned and claim of the present invention is protected make selection criterion known in the art to use without restriction in the condition of all not having special exceptions aspect its size, shape, material selection or the technological design.
Other details of theme of the present invention, feature and advantage are by visible in the describing below of dependent claims and relevant drawings and table, wherein as the embodiment of describing exemplary sintering belt gas purification.
Description of drawings
Figure 1A illustrates the sketch map of the method (flow chart) of first embodiment;
Figure 1B illustrates the sketch map of the method (flow chart) of second embodiment;
Fig. 2 is with the single reactor assemblies of perspective vertical cross-section signal;
Fig. 3 is as two reactor assemblies that stack is arranged than large scale sintering waste gas purification apparatus part.
The specific embodiment
In the embodiment of Figure 1A, be sent in the in fact known electrofilter 20 through pipeline 11 at the waste gas that produces on the sintering belt 10.Consequent dust sends back sintering belt through pipeline 12.Get into the rearmounted air blast 14 through pipeline 13 with about 150-165 ℃ of waste gas that flows out from electrofilter.This provides enough superchargings for the device operation.The sintered discharge gas that leaves through pipeline 15 at first passes through water evaporative cooling to about 135 ℃, and discharges plate 52B through the gas inflow/bulk material that air blast 14 ' imports in the moving-burden bed reactor 50 of adverse current operation.Purge gas through pipeline 16 is derived can directly be sent into waste stack 60, and enters atmosphere.If desired, electrofilter 20 can replenish through bag hose 20A and filter or replace with bag hose 20A.
The bulk material layer 54A/B that in moving bed reactor device 50, is provided with is made up of for example activated charcoal particle.Also passed the dust residue of electrofilter 20 and/or bag hose 20A; Comprise mercury and other heavy metal and possible other pollutant such as organic compound; Particularly heavy hydrocarbon 、 bioxin and furans etc. are directly becoming a mandarin the district, promptly flow into plate 52B in the bottom and deposit through absorption, absorption or adhesion with the stratum granulosum district that possibly be located immediately on it.From absorption and/or the 54B of absorbent lower floor, sintered discharge gas turns to position 57 to discharge from reactor 50 in side, and in the axial clearance with NH 3Thoroughly fully mix.Then, the inflow of sintered discharge gas arrival reactor 50/below the discharge plate 52A, and upwards get into absorption and/or absorbent upper strata 54A with denitrogenation.Following in the face of Fig. 2 and 3 is explained, in succession through two adsorbent layer 54A/B, and arrive outlet downwards through the absorption of storage bin hopper 56 feed and/or absorbent.In the 54A of adsorbent upper strata, sintered discharge gas still basically only contains NO x、 bioxin/furans or any other pollutant such as PCB and/or PAK, then these materials with combine from top adsorbent or absorbent fresh or regeneration.Under the catalytic action of activated charcoal, by NO xAnd NH 3Basically form steam and nitrogen.NH 3NH therein 4OH spray into and the device 40 that mixes with compressed air in produce.The NH of tool original creation meaning 3Add preferably operation as follows of unit 40:
25% NH 4OH solution mixes at 40A with compressed air.Mixture is inner through the evaporimeter that pipeline arrives nozzle plate 40B (for example porous plate) below.Upside at the inner nozzle plate 40B of this evaporimeter receives air-NH 4The OH mixture impacts, and this mixture is evenly distributed on evaporimeter inside through nozzle plate.This mixture is by the abundant preheating of heat exchanger 40C.The NH that supplies with by mixed zone 40A among the atomizer 40D of nozzle plate 40B below 4OH and compressed-air actuated without adding air-NH that hot mixt mainly is positioned at the warp heating on the nozzle plate 40B 4OH mixture evaporation makes air/H 2O steam/NH 3Mixture gets into feeder sleeve 40E in the evaporimeter lower end down at about 120 ℃, and this feeder sleeve is that turning to of moving-burden bed reactor 50 distinguishes 57, turns to the contact said mixture at this sintered discharge gas.
The activated charcoal of using is sent into screening plant 80 through pipeline 17; The fine material that sifts out once more (material of undersize) gets into the fuel combustion of sintering belt as sintering process through pipeline 17 '; And the coarse material that is produced is through pipeline 17 " get in fact known regenerator section 70, the material of undersize can not turn back to moving-burden bed reactor 50 thus.This regenerator section 70 is made up of multistage reactor, and the activated charcoal of load is from top to bottom through this reactor.In the preparatory degasification section 70A of top, activated charcoal is heated to about 450 ℃.In postmedian degassing stages 70C, remove the rich SO of gathering 2Gas also is sent to disposal plant with it through pipeline 19, like sulfuric acid production plant 90, among the cooling section 70B that follows downwards, only has a spot of pollutant still to disengage.From regeneration unit 70, the storage bin hopper 56 that will send moving-burden bed reactor 50 again back to through pipeline 18 through absorption and/or the absorbent of regeneration.Details are as follows to have the operation of regeneration unit 70 of original creation meaning:
From the activated charcoal of using of moving-burden bed reactor 50 through screening plant 80 and pipeline 17 " arrive superposed storage bin hopper 71.Be positioned at following regenerator section 70A and be designed to the tubular type desorption device, many downward VERTICAL TUBE are promptly arranged in the bottom of storage bin hopper 71, activated charcoal can move through these pipes, and these Guan Zaiqi outsides are by about 450 ℃ hot combustion air heating simultaneously.In the lower end of regenerator section 70A, these pipes get in the chamber (regenerator section 70C) of cross section expansion through the plate of bottom, and this chamber receives activated charcoal as the back degas zone, and it stopped about 1-2 down individual hour at about 450 ℃ in the chamber.The lower end of the degas zone in the back of the activated charcoal through whole regenerator section arrives tubular reactor (regenerator section 70B) again gradually from the top down, and the structure type of this tubular reactor corresponds essentially to the tubular type desorption device of regenerator section 70A.Activated charcoal by cooling indirectly, wherein is used in the outside of cooling tube at this as the air at room temperature of cold gas.In the lower end of regenerator section 70B, carry the pipe of activated charcoal once more it freely to be discharged in the plate.Activated charcoal gets into the discharge bucket 72 that places the below thus.Regenerator section 70B lower end do not contacting with the compressed air of 20 ° of introducings with activated charcoal be sent to down regenerator section 70C below.To provide the heater 73 of air and combustion gas at the air guide of cooling section preheating at this pipeline.Combustion gas/the air mixture of heat is not directly contacting the lower end that arrives regenerator section 70A down with activated charcoal then, and temperature is still left regeneration unit 70 for about 450 ℃ air in the upper end of regenerator section 70A once more.
Arrive pollutant desorb under given temperature conditions and indirect of bringing-up section 70A with the activated charcoal of load, and can be in the back degas zone 70C through pipeline 19 and through storage bin hopper 71 and pipeline 19 ' as rich SO 2Gas leaves regeneration unit 70, drawing-in type air blast 19A produces required decompression also further with rich SO 2Gas is sent to for example in fact known sulfuric acid production plant 90 with further processing.Promote the activated charcoal of heat in outside desorption tube of being heated in the regenerator section 70A of top to shift to the stripping gas that pipeline 19 ' rises.But also can be about to nitrogenous sweep gas and be transported in the storage bin hopper 71, and this sweep gas is imported back degas zone 70C and from then on is sent to sulfuric acid apparatus 90 through desorption tube with the dotted line pipeline 74 among the figure as replacement scheme.To conduct heat in order also in cooling section 70B, from activated charcoal, discharging to contain the gas of pollutant and in this cooling section, to promote, to impact through the nitrogenous sweep gas of pipeline 75 usefulness and discharge bucket 72, this sweep gas again through after degas zone 70C from regeneration unit 70 discharges.
Expressing the typical flue gas of waste gas purification front and back down forms:
Unstripped gas The gas that purified
Bioxin 3-10 0.1-0.5 ng/m 3
SO 2 700 ＜50 mg/m 3
HCl 50 ＜5 mg/m 3
NO x 350 ＜100 mg/m 3
First embodiment:
Adopt the service condition (not using bag hose) that provides among Figure 1A in the first embodiment.
Second embodiment:
In second embodiment, adopt the service condition that provides among Figure 1B (when using bag hose, all the other be provided with Figure 1A in identical).
In the embodiment of Figure 1B, particularly activated charcoal consumption, activated charcoal amount to be regenerated and the H of generation 2SO 4Amount all is significantly less than the embodiment of Figure 1A.
Visible by Fig. 2, moving-burden bed reactor 50 the simplest forms of the present invention are made up of the container 50A of rectangular profile, replenish activated charcoal, the storage bin hopper 56 of this activated charcoal above being arranged in the upper end of container 50A.Activated charcoal is fed to activated charcoal upper strata 54A through bulk material distribution plate 50C with the bulk material distributing pipe 50B of matrix arrangement thus.This accomplishes under unobstructed unit or closing device, makes pure gravity capable of using fill, and finishes if the surperficial 50A ' on activated charcoal upper strata filled automatically when arriving the outlet side of bulk material distributing pipe 50B.Between the bulk material distributing pipe, form gas with the known mode of reality and discharge the space.In the lower end of activated charcoal upper strata 54A, there are for example inflow of the upper gas of actual known tactic pattern and bulk material discharge plate 52A from WO 88/08746 A1.Bulk material moves down through this upper board 52A, and sintered discharge gas upwards flows.The bulk material discharge pipe 52C that the bulk material of arranging with matrix form is discharged behind the funnel passes intermediate plate 53, and bulk material freely is discharged into the upper surface of the activated charcoal layer 54B below it.Here be not provided for the blocking unit or the closing device of activated charcoal yet.There is the lower gas of similar plate 52A structure to flow into and bulk material discharge plate 52B in the lower end of the 54B of activated charcoal lower floor.Downward bulk material discharge pipe 52D behind matrix form passes intermediate plate 55, is provided with single bulk material deliverying unit of the device for transferring 58 of whole assembly below the intermediate plate.This deliverying unit is known from WO 90/14156 A1 especially.The activated charcoal of load shifts out in the reactor lower end.
Sintered discharge gas to be clean turns to district 57 to discharge intermediate plate 55 edges, with NH 3Thoroughly fully mix, and get into the bulk material upper strata 54A of the moving-burden bed reactor 50 below gas inflow/bulk material is discharged plate 52B.
Visible by Fig. 3, moving-burden bed reactor 50 also can be configured to two-stage.So it is made up of two mutual stacked assemblies with structure shown in Figure 2 basically.In Fig. 3, the Reference numeral of lower component is added with '.In order to make the absorption and/or the conveying of absorbent simple; Bulk material carrier pipe 59A begins to arrange from storage bin hopper 56; Pass completely through the top of two moving-burden bed reactor assemblies; And below device for transferring 58 Y-shaped being distributed on the bottom storage bin hopper 56 ', wherein intermediate plate 51 is used for the fresh absorption that flows into bottom storage bin hopper 56 ' and/or absorbent and absorption and/or absorbent in the load of device for transferring 58 discharges are separated fully.The absorption of the load of this upper reactor assembly and/or absorbent pass completely through the bottom reactor assemblies through bulk material carrier pipe 59B; Arrive thus and discharge funnel 59C, the absorption of the load of these two reactor assemblies and/or absorbent are discharged funnel through this and are discharged from moving-burden bed reactor 50.
The device of the reality of Fig. 4 is executed instance the general execution situation by the technology of Figure 1A is shown, and wherein similar parts are represented with identical Reference numeral.With the difference of Figure 1A be:
-the device that is used to purify sintering belt waste gas is the binary channels formula:
-electrofilter 20 has several zones, is 5 here, in the combination of being considered, before bag hose, inserts 2 or 3 zones;
-bag hose has many chamber 20A ', the bag hose chamber 20A ' that has 4 parallel connections to use here, and each has a plurality of filter bag;
-behind air blast 14, bag hose 20A and moving-burden bed reactor 50 can be bypassed to chimney 60 through pipeline 22, to avoid interference under special circumstances or impaired;
-additional air blast 14 ' produces required superpressure overcoming the pressure loss in the back moving-burden bed reactor assembly 50 ', and about illustrating in the moving-burden bed reactor component drawings 2, and it also can be configured to multistage.
In order waste gas to be cooled to the desirable running temperature in the waste gas purification apparatus, can to sneak into surrounding air and/or spray into water with evaporative cooling.Before this is sneaked into and/or sprays into the position and can be positioned at one/a plurality of electrofilters and/or bag hose.Occur or occur under the special running status increasing and the still sintering belt of viscosity at pollutant, can in waste gas stream, add known granular material to capture pollutant.This can be before electrofilter, bag hose and/or moving-burden bed reactor (filter) carry out wherein this material single cycle or conveying before
At the sintering belt waste gas purification apparatus of the gas stream that is used for very big volume, can realize improved flexibility in the distribution (managing 11A, 15A, 17A and possible blocking unit) in electrofilter, bag hose and/or assembled moving bed bioreactor assembly and/or a plurality of parts through changing gas.
In the present invention, the characteristic in the accompanying drawing can single or mutual Combination application, and this is all in the framework of single embodiment of the present invention and various embodiment.
Reference numerals list:
10 sintering belts
11 pipelines
12 pipelines
13 pipelines
14 air blasts
15 pipelines
16 pipelines
17 pipelines
17 ' pipeline
17 " pipeline
18 pipelines
19 pipelines
19 ' pipeline
The 19A air blast
20 electrofilters
The 20A bag hose
40 NH 3Add the unit
The 40A mixed zone
The 40B nozzle plate
The 40C heat exchanger
The 40D atomizer
The 40E feeder sleeve
50 moving-burden bed reactors
The 50A container
50A ' surface
50B bulk material distributing pipe
50B ' surface
50C bulk material distribution grid
50C ' bulk material distribution grid
51 intermediate plates
52A, 52A ' top inflow/discharge plate
52B, 52B ' bottom inflow/discharge plate
52C bulk material discharge pipe
52D bulk material discharge pipe
53,53 ' intermediate plate
54A, 54A ' bulk material upper strata
54B, 54B ' bulk material lower floor
55,55 ' intermediate plate
56 storage bin hoppers
56 ' bottom storage bin hopper
57,57 ' turns to the district
58,58 ' device for transferring
59A/B bulk material carrier pipe
59C discharges funnel
60 chimneys
70 regeneration units
70A, B, C regenerator section
71 storage bin hoppers
72 discharge bucket
73 heaters
74 pipelines
75 handle money
80 screening plants
90 sulfuric acid production plants

Claims (41)

1. method that is used to purify the waste gas of partial combustion technology at least, wherein the part solid fuel experiences the partial combustion at least of said solid at least, and wherein said waste gas removes and contains CO 2, CO, O 2, H 2O and/or N 2Outer at least some in the following pollutant: the NO that also contains x, SO 2, HCl, HS, Hg, two English, furans, dust and be derived from distilling or condensable residue, heavy hydrocarbon and/or heavy metal of the technology of glowing, said method be characterised in that,
-make waste gas, possibly be the waste gas after the preparatory dust removal step, from following entering moving-burden bed reactor, discharge plate through the inflow of lower horizontal gas and the bulk material of said moving-burden bed reactor, get into by NO xAnd SO xAnd/or the absorption of other contaminants and/or absorbent lower floor, when flowing through said absorption and/or absorbent lower floor, the SO of the main at least amount in the waste gas xBy load NO is arranged with other possible pollutant xAnd/or N 2The pore system of absorption and/or absorbent adsorbed,
-mainly measure SO xThe waste gas that is cleaned with other possible pollutant leaves said lower floor from the last Free Surface of said absorption and/or absorbent lower floor, then fully to mix with ammonium-containing compound, is used to transform NO x,
-mix with said ammonium-containing compound and mainly measure SO xAnd/or the waste gas that possible pollutant is cleaned is from following entering, and the upper level gas that flows through said moving-burden bed reactor flows into bulk material discharges plate, and entering is by NO xAnd/or N 2And possible a small amount of SO xWith the absorption and/or the absorbent upper strata of possible other contaminants, when flowing through said absorption and/or absorbent upper strata, the NO of the main at least amount in the said waste gas xComposition and/or its product are adsorbed on load has NO xAnd/or N 2With possible a small amount of SO xOn the surface of the absorption of possible other pollutant and/or absorbent,
-mainly measure SO xWith possible other pollutant and NO xThe waste gas that composition is cleaned leaves said upper strata from the last Free Surface on said absorption and/or absorbent upper strata, leaves said process subsequently,
-with fresh and/or through the absorption of regeneration and/or absorbent through the bulk material distribution grid of said moving-burden bed reactor upper end from the last last Free Surface that is added to said absorption and/or absorbent upper strata evenly distributedly; In upper gas inflow and bulk material discharge plate district, do not interrupted by blocking unit; Then the upper and lower through whole moving-burden bed reactor fully from the top down little by little, load NO at first in its surface one after the other thus xOr N 2And steam, load SO in its pore system subsequently xWith other possible pollutant, the lower gas through said moving-burden bed reactor flows into and bulk material discharge plate then,
Subsequent delivery, discharge and the translational speed of-said absorption and/or absorbent be through flowing in said lower gas and bulk material is discharged below the plate or carried out at the bulk material deliverying unit that said lower gas flows into and bulk material is discharged on the plate, and
-said absorption and/or absorbent in the upper strata of said moving-burden bed reactor to SO xWith the load capacity of possible other pollutant through corresponding be controlled at said lower gas flow into discharge below the plate with bulk material or said lower gas flow into and bulk material discharge plate on the bulk material deliverying unit be adjusted to the amount that can be scheduled to respect to the absorption and/or the absorbent of load.
2. the method for claim 1 is characterized in that, with the absorption of said moving-burden bed reactor and/or absorbent on the upper strata to SO xThe weight that is limited in by absorption of on said bulk material deliverying unit, discharging and/or absorbent with the load value of possible other pollutants is 10 weight % to the maximum.
3. the method for claim 2 is characterized in that, with the absorption of said moving-burden bed reactor and/or absorbent on the upper strata to SO xThe weight that is limited in by absorption of on said bulk material deliverying unit, discharging and/or absorbent with the load value of possible other pollutants is 6 weight % to the maximum.
4. claim 1 or 2 method is characterized in that, use carbon containing absorption and/or absorbent as said absorption and/or absorbent.
5. the method for claim 4 is characterized in that, said carbon containing absorption and/or absorbent are activated charcoals.
6. the method for claim 5 is characterized in that, said carbon containing absorption and/or absorbent are the activated charcoals of moulding.
7. the method for claim 4 is characterized in that, the granularity of said carbon containing absorption and/or absorbent is mainly 1-10mm.
8. the method for claim 7 is characterized in that, the granularity of said carbon containing absorption and/or absorbent is mainly 3-8mm.
9. the method for claim 7 is characterized in that, the granularity of said carbon containing absorption and/or absorbent is mainly 4-6mm.
10. the method for claim 4; It is characterized in that; Absorption and/or the absorbent consumption of below said moving-burden bed reactor, discharging or that part consumes are removed pollutant adsorbed and/or that absorbed in a large number a regeneration step, and part is mixed mutually from the top separately or with the carbon containing absorption of fresh use and/or absorbent and sent into the said moving-burden bed reactor as absorption and/or absorbent again at least.
11. the method for claim 4 is characterized in that, uses carbon containing absorption and/or the absorbent of preparatory activator as fresh use.
12. the method for claim 4 is characterized in that, carries out under greater than 80 ℃ temperature in the gas purification on said absorption and/or the absorbent.
13. the method for claim 12 is characterized in that, carries out under 80-180 ℃ temperature in the gas purification on said absorption and/or the absorbent.
14. the method for claim 12 is characterized in that, carries out under 100-150 ℃ temperature in the gas purification on said absorption and/or the absorbent.
15. the method for claim 4 is characterized in that, the height on absorption in the said moving-burden bed reactor and/or absorbent upper strata is 1.5-4.5m.
16. the method for claim 15 is characterized in that, the height on absorption in the said moving-burden bed reactor and/or absorbent upper strata is 2.5-3.5m.
17. the method for claim 15 is characterized in that, the height on absorption in the said moving-burden bed reactor and/or absorbent upper strata is about 3m.
18. the method for claim 4 is characterized in that, the height of absorption in the said moving-burden bed reactor and/or absorbent lower floor is 0.5-3m.
19. the method for claim 18 is characterized in that, the height of absorption in the said moving-burden bed reactor and/or absorbent lower floor is 1.5-2m.
20. the method for claim 18 is characterized in that, the height of absorption in the said moving-burden bed reactor and/or absorbent lower floor is about 1.75m.
21. a method that is used to purify the waste gas of partial combustion technology at least, wherein the part solid fuel experiences the partial combustion at least of said solid at least, and wherein said waste gas removes and contains CO 2, CO, O 2, H 2O and/or N 2Outer at least some in the following pollutant: the NO that also contains x, SO 2, HCl, HS, Hg, two
Figure FSB00000686068800031
English, furans, dust and be derived from distilling or condensable residue, heavy hydrocarbon and/or heavy metal of the technology of glowing is characterized in that, are used for NO xTransform and be adsorbed on ammonium-containing compound on the bulk material by containing the preparation of ammonium salt solution and compressed-air actuated mixture, said mixture is sprayed to the another kind that contains ammonium salt solution and air in the evaporimeter in the mixture of heating, formation air/H 2O steam/NH 3Gas mixture.
22. the method for claim 1 is characterized in that, is used for NO xTransform and be adsorbed on ammonium-containing compound on the bulk material by containing the preparation of ammonium salt solution and compressed-air actuated mixture, said mixture is sprayed to the another kind that contains ammonium salt solution and air in the evaporimeter in the mixture of heating, formation air/H 2O steam/NH 3Gas mixture.
23. the method for claim 21 or 22 is characterized in that the said ammonium salt solution that contains is NH 4OH solution.
24. a method that is used to purify the waste gas of partial combustion technology at least, wherein the part solid fuel experiences the partial combustion at least of said solid at least, and wherein said waste gas removes and contains CO 2, CO, O 2, H 2O and/or N 2Outer at least some in the following pollutant: the NO that also contains x, SO 2, HCl, HS, Hg, two
Figure FSB00000686068800041
English, furans, dust and be derived from distilling or condensable residue, heavy hydrocarbon and/or heavy metal of the technology of glowing; It is characterized in that; Carry out regeneration step with 3 step process, wherein at first will be from the vertically extending regeneration unit of last introducing, through the desorption device of indirect from the activated charcoal of the load nitrogen of said moving-burden bed reactor; Then from passing through the dusty gas of back degas zone, at last from cooler through indirect cooling with the sucking-off desorb.
25. the method for claim 1; It is characterized in that; Carry out regeneration step with 3 step process, wherein at first will be from the vertically extending regeneration unit of last introducing, through the desorption device of indirect from the activated charcoal of the load nitrogen of said moving-burden bed reactor; Then from passing through the dusty gas of back degas zone, at last from cooler through indirect cooling with the sucking-off desorb.
26. the method for claim 24 or 25 is characterized in that, the desorption device of said indirect is the tubular type desorption device.
27. the method for claim 1 is characterized in that, carries out the preliminary clearning step, in said waste gas, add to be selected from calcium oxide, calcium hydroxide, sodium acid carbonate and/or similarly alkali metal or alkaline earth metal compound, with part SO x, HS and/or HCl combine.
28. the method for claim 27 is characterized in that, before bag hose, in said waste gas, adds to be selected from calcium oxide, calcium hydroxide, sodium acid carbonate and/or similar alkali metal or alkaline earth metal compound.
29. the method for claim 27 or 28 is characterized in that, addition is corresponding to the stoichiometric factor that is 1.0-2.5.
30. the method for claim 29 is characterized in that, said stoichiometric factor is 1.5-2.0.
31. the method for claim 27 or 28 is characterized in that, the SO that in said preliminary clearning step, removes x, HS and/or HCl amount be contained SO in the said waste gas x, HS and/or HCl 10-90%.
32. the method for claim 31 is characterized in that, the SO that in said preliminary clearning step, removes x, HS and/or HCl amount be contained SO in the said waste gas x, HS and/or HCl 50-80%.
33. the method for claim 31 is characterized in that, the SO that in said preliminary clearning step, removes x, HS and/or HCl amount be contained SO in the said waste gas x, HS and/or HCl 65-75%.
34. a device that is used to purify the waste gas of partial combustion technology at least, wherein the part solid fuel experiences the partial combustion at least of said solid at least, and wherein said waste gas removes and contains CO 2, CO, O 2, H 2O and/or N 2Outer at least some in the following pollutant: the NO that also contains x, SO 2, HCl, Hg, two
Figure FSB00000686068800051
English, furans, dust and be derived from distilling or condensable residue, heavy hydrocarbon and/or heavy metal of the technology of glowing,
Said device is characterised in that,
-have lower horizontal gas to flow into and bulk material discharge plate (52B; 52B ') be filled with the absorption and/or the moving-burden bed reactor (50) on absorbent lower floor and upper strata, said waste gas under can be through said lower gas inflow and bulk material discharge plate (52B; 52B ') flows into by NO xAnd/or N 2And SO xAbsorption and/or the (54B of absorbent lower floor with possible other contaminants; 54B '),
-be placed on the mixed cell of the last Free Surface (50B ') of said absorption and/or absorbent lower floor, be used to make main amount SO xThe waste gas that is cleaned with other possible pollutant fully mixes with ammonium-containing compound,
The upper level gas of-said moving-burden bed reactor flows into and bulk material is discharged plate (52A; 52A '), flow into and bulk material discharge unobstructed unit, plate district the main amount SO that mixes with ammonium-containing compound in said upper gas xThe waste gas that is cleaned with other possible pollutant can flow into and bulk material discharge plate (52A through said upper gas; 52A ') from flowing into by NO down xOr N 2With a small amount of SO xAnd the absorption of other possible contaminants and/or absorbent upper strata (54A; 54A '),
-said absorption and/or absorbent upper strata (54A; Last Free Surface 54A ') (50A '), said main amount SO xWith possible other pollutant and NO xThe waste gas that composition is cleaned can from
Said upward Free Surface (50A ') leave said absorption and/or absorber layer, leave said moving-burden bed reactor (50) subsequently,
-at the bulk material distribution grid (50C) of moving-burden bed reactor upper end, absorption fresh and/or regeneration and/or absorbent can be through the last Free Surface on said absorption and/or absorbent upper strata from last supplies, and can evenly distribute through said plate,
-flow into and bulk material discharge plate (52B in said lower gas; 52B ') last or bulk material deliverying unit (58 thereunder; 58 '), can realize subsequent delivery, discharge and the translational speed of said absorption and/or absorbent through it,
The control module of-said bulk material deliverying unit, the upper strata (54 of said moving-burden bed reactor; 54A ') absorption in and/or the SO of absorbent xCan be controlled at said lower gas and flow into and bulk material discharge plate (52B through corresponding with the load capacity of possible other pollutant; 52B ') discharges the bulk material deliverying unit (58 on the plate below or in said lower gas inflow and bulk material; 58 ') be adjusted to the amount that to be scheduled to respect to the absorption and/or the absorbent of load.
35. the device of claim 34 is characterized in that, is used for mainly measuring SO xThe gap nozzle that approximate horizontal is extended at least one wall that waste gas that is cleaned with other possible pollutant and the well-mixed mixed cell of ammonium-containing compound are included in said moving-burden bed reactor.
36. a device that is used to purify the waste gas of partial combustion technology at least, wherein the part solid fuel experiences the partial combustion at least of said solid at least, and wherein said waste gas removes and contains CO 2, CO, O 2, H 2O and/or N 2Outer at least some in the following pollutant: the NO that also contains x, SO 2, HCl, Hg, two
Figure FSB00000686068800061
English, furans, dust and be derived from distilling or condensable residue, heavy hydrocarbon and/or heavy metal of the technology of glowing is characterized in that NH 3Add unit (40), be used for NO with the preparation of said unit xTransform and be adsorbed on the ammonium-containing compound on the bulk material; It has and contains ammonium salt solution and compressed-air actuated mixed zone, is used for heating the heat exchanger of another mixture that contains ammonium salt solution and air and is used to make first mixture and through the spray nozzle that mixes at evaporimeter of second mixture of heating, to form air/H 2O steam/NH 3Gas mixture.
37. the device of claim 34 is characterized in that NH 3Add unit (40), be used for NO with the preparation of said unit xTransform and be adsorbed on the ammonium-containing compound on the bulk material; It has and contains ammonium salt solution and compressed-air actuated mixed zone, is used for heating the heat exchanger of another mixture that contains ammonium salt solution and air and is used to make first mixture and through the spray nozzle that mixes at evaporimeter of second mixture of heating, to form air/H 2O steam/NH 3Gas mixture.
38. the device of claim 36 or 37 is characterized in that the said ammonium salt solution that contains is NH 4OH solution.
39. a device that is used to purify the waste gas of partial combustion technology at least, wherein the part solid fuel experiences the partial combustion at least of said solid at least, and wherein said waste gas removes and contains CO 2, CO, O 2, H 2O and/or N 2Outer at least some in the following pollutant: the NO that also contains x, SO 2, HCl, Hg, two
Figure FSB00000686068800062
English, furans, dust and be derived from distilling or condensable residue, heavy hydrocarbon and/or heavy metal of the technology of glowing; It is characterized in that being used for the regeneration unit of 3 step desorption techniques; The activated charcoal that pollutant wherein will be arranged from the load of said moving-burden bed reactor (50) is at first from sending into vertically extending regeneration unit (70); Through the desorption device of indirect, then from passing through the dusty gas of back degas zone, at last from cooler through cooling off indirectly with the suction desorb.
40. the device of claim 34; It is characterized in that being used for the regeneration unit of 3 step desorption techniques; The activated charcoal that pollutant wherein will be arranged from the load of said moving-burden bed reactor (50) is at first from sending into vertically extending regeneration unit (70); Through the desorption device of indirect, then from passing through the dusty gas of back degas zone, at last from cooler through cooling off indirectly with the suction desorb.
41. the device of claim 39 or 40, the desorption device that it is characterized in that said indirect are the tubular type desorption devices.
CN2007800513602A 2006-12-14 2007-12-14 Method and device for purifying the flue gases of a sintering process of ores and/or other metal-containing materials in metal production Active CN101605589B (en)

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PCT/EP2006/012062 WO2008071215A1 (en) 2006-12-14 2006-12-14 Method and device for scrubbing effluent gases from a sintering process for ores or other metal-containing materials in metal production
PCT/EP2007/011048 WO2008071446A1 (en) 2006-12-14 2007-12-14 Method and device for purifying the flue gases of a sintering process of ores and/or other material-containing materials in metal production

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